US2669538A - Separation of vapors and viscous liquids - Google Patents

Separation of vapors and viscous liquids Download PDF

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Publication number
US2669538A
US2669538A US77172A US7717249A US2669538A US 2669538 A US2669538 A US 2669538A US 77172 A US77172 A US 77172A US 7717249 A US7717249 A US 7717249A US 2669538 A US2669538 A US 2669538A
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United States
Prior art keywords
stream
mass
propane
zone
separation
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Expired - Lifetime
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US77172A
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English (en)
Inventor
Frank H Yurasko
Howard C North
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Standard Oil Development Co
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Standard Oil Development Co
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Priority to BE493780D priority Critical patent/BE493780A/xx
Application filed by Standard Oil Development Co filed Critical Standard Oil Development Co
Priority to US77172A priority patent/US2669538A/en
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/003—Solvent de-asphalting
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D19/00—Degasification of liquids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D19/00—Degasification of liquids
    • B01D19/0042—Degasification of liquids modifying the liquid flow
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D19/00—Degasification of liquids
    • B01D19/0068—General arrangements, e.g. flowsheets

Definitions

  • the present invention is concernedwith an improved "refining operation and'ismore'specii'lcally concerned with ya method for-securing the gradual dissipation'cf the'energyof flowing streams.
  • the invention is-especially directed toward the handling 0i' vilowing--strearns whereby the energy ofthe ilowing streamisdissipated and various phases segregated.
  • viscous liquid streams containing entrained vaporous constituents arehandled ina manner to eiiciently dissipatefthe Viiowing energy and to segregate'or separate the vaporous constituents from the viscous-liquid.
  • Thev heated liquid asphalt stream containing vaporous solvent is .introduced into a separation zone which usually comprises a 'iiash separation zone.
  • a separation zone which usually comprises a 'iiash separation zone.
  • ⁇ phase due tothe viscousnature of the liquid, ⁇ phase, -itis relatively difficult to secure a complete and satisfactory separation of the vaporous constituents.
  • One. .expedient Which ⁇ has'been utilized in an Vattempt to minimize 'this problem is to lemploy relatively large separation zones and also to'utilizein (Cl. ISG-1.14146) conjunction therewith vabalileplate or similar types-structures.
  • the incoming stream is impinged-against the -balile'plate-or caused .to circulatearound the. periphery of the ash zone.
  • the iioWing stream is fiinely shredded ⁇ intoa multiplicity of streams and the energy of the entire mass'dissipated progressively.
  • the present invention is ⁇ particularly adapted for the manufactureof .high-quality asphalts. .
  • the invention may be readily understood by reference to theidrawings 'illustrating embodiments of ⁇ the same.
  • Figure'v 1 illustrates one embodiment of the invention Tas itis applied to the manufacture of highzqualitypetroleum asphalta'while
  • Figure 2 illustrates :in'somedetail .the'characterof the lamentousmaterial.
  • Ii propane' be employed, as 4a solvent, a desirable feedfis in the'range .fromabout Gato 10 volumes ⁇ of pro pane per yolumexof oilizfeed.
  • The-temperature maintained in the bottom ofy .the propane tower is in ⁇ the Vrange'from about 100' yto 120 F., While the r-top-temperature -is inthe range Ifrom about to'-1'60-F. 1 It is tobe understood thatsuit 3 able contacting and distributing means may be employed within the tower itself.
  • the oil-solvent stream is removed from the top of zone l by means of line 3, further heated in heating zone 4 to a temperature above the vaporization temperature of the propane at the existing pressure and introduced into a flash separation Zone 20.
  • Vaporized propane is removed overhead from zone by means of line 5 while the oil stream still containing a relatively small amount of vaporized propane is removed from zone 20 by means of line 6.
  • this stream is introduced into zone by impinging the flowing stream onto and into a mass of fibrous material 40 which preferably comp prises a mass of line woven wire. This mass of woven wire is maintained at the top of distillation zone 30 and is disposed approximately from about 6 to 18" away from the end of line B.
  • the incoming stream containing vaporous and liquid constituents is shredded into a multiplicity of streams of minute diameter under conditions that the vaporous constituents are effectively and efficiently separated from the liquid constituents in the absence of any foaming whatsoever.
  • Oil constituents completely free of propane are with drawn from the bottom of zone 30 by means of line l', and handled or further refined in any manner desired.
  • the freed vaporous propane is withdrawn from the top of Zone 30 by means of line B, and preferably passed through a compressor zone 50.
  • the compressed propane is removed from zone 50 by means of line Si, passed through a condensing zone S0 and preferably recycled to the system by means of line I4.
  • the asphalt-solvent stream is removed from depropanizing tower i0 by means of line H, passed through heating unit l2 which is mainn tained at a temperature above the vaporization point of the solvent.
  • This stream is introduced into zone 50 in a manner to impinge the stream into a web-like mass of material, preferably into a mass of wire 'l0 maintained at the top of tower 60.
  • the asphalt stream containing entrained vaporous propane is shredded into a multiplicity of streams of very small diameters.
  • the freed propane is withdrawn overhead from zone i by means of line I3 and is preferably combined with the propane removed overhead from zone 20. This combined stream is combined with the compressed propane stream removed from Zone 50 prior to passing the combined streams to condenser B0.
  • a bottoms stream of asphalt containing a relatively small amount of propane is withdrawn from zone 60 by means of line i5 and introduced into Zone 90.
  • the asphalt stream is directed into a mass of woven or equivalent material which preferably comprises a mass of Wire.
  • the energy of the stream is gradually dissipated, the propane released and is removed overhead by means of line I6.
  • This stream is preferably combined with the overhead propane stream removed from zone 30 by means of line 8.
  • An asphalt stream completely free of propane is removed from zone 90 by means of line Il and handled or further refined as desired.
  • Figure 2 illustrates in some detail the character of the filamentous mass 'l0 supported in the vapor space of zone 60 by means of suitable supports 5I.
  • the mass may be of any suitable material, but it is preferred that it be of a metal as for example, fine wire having a composition adapted to specically resist the corrosion of any particular corrosive stream.
  • the mass is preferably of a spongy or of a resilient nature.
  • the amount of mass of wire or equivalent material utilized may vary appreciably depending upon the velocity of the particular stream it is being used in conjunction with, as well as, upon the diameter of the stream and also upon the actual chemical and physical characteristics of the flowing stream.
  • the face of the mass approximate a rectangle having sides from about 9" to 20" and that the thickness of the mass vary in the range from about 3" to 12".
  • the mass be approximately 6 to 9" thick and that it be disposed from about 2 to 18l away from the inlet of the flowing stream in a manner that the stream will impinge at right angles on the face of the mass.
  • the process is directed toward the eflicient releasing of an entrained vapor phase from a liquid phase. This is accomplished by shredding the liquid phase containing the entrained vapor phase into a multiplicity of very fine streams thus releasing the vaporous constituents.
  • a direct application 01- the present invention is in the manufacture ofA heavy viscous products.
  • Example An asphaltic reduced crude was countercurrently contacted in a propane tower wherein about 8 volumes of propane were used per volume of oil.
  • the temperature at Ithe top of the tower was maintained at about 150 F., while the temperature in the bottom of the tower was maintained at about 110 F. Under these conditions approximately 75% of the oil based upon feed was removed from the top of the tower.
  • the ratio of propane to oil in this stream was approximately 12 to l.
  • This stream was heated to about 400 F. and flashed under conditions to remove overhead a large amount of the propane.
  • the oil stream at about 350 F. and containing about 10% of propane was introduced into the top of a depropanizing tower.
  • this stream was impinged onto and into a mass of steel wire, the dimensions of which were about 12" x 12 x 6".
  • the free space of the mass employed was about 95%. Under these conditions substantially no emulsiiication of the oil occurred and a rapid and erhcient separation of the propane was secured. When this method was not utilized with respect to this stream emulsication dihiculties occurred and it was relatively diflicult to secure complete removal of the propane from the oil phase.
  • the stream withdrawn from the bottom of the solvent treating tower comprised about 25% of the oil feed.
  • the ratio of propane to oil in this stream was approximately 1/1.
  • This stream was heated to a temperature of about 450 F. and flashed into an initial separation zone wherein substantially all of the propane was removed from the asphaltic constituents.
  • the stream was impinged upon a mass of steel wire, the dimensions of which were about 12 X 12" X 6".
  • the mass of steel wire comprised approximately 95% of free space.
  • An asphalt stream was withdrawn from the bottom of the initial separation zone at a temperature of about 450 F.
  • This stream contained approximately 5% propane.
  • this stream was introduced into the top of a depropanizing tower and impinged onto a mass of ine steel wire having dimensions of about 12" X 12" X 6".
  • the amount oi free space in the mass itself was about 95%.
  • Rapid and eiiicient separation of the propane was secured from the asphaltic constituents.
  • the propane was removed overhead while the asphalt stream free of propane was removed from the bottom of the zone.
  • the incoming stream emulsications problems were encountered. It was also relatively dicult to remove all of the propanefrorn the productos-L phalt stream.
  • the invention is broadly concerned with a process ⁇ for the gradualdissipation of energy. of a iiowing stream, particularly when the owing stream isl introduced into:l a vessel of larger diam-eter. by utilizing a mass of nely woven material ⁇ in. order to shred the flowing. streamv into a multi. ⁇ plicity of ne streams.
  • the invention is particularly adapted for the segregation. of' vaporous constituents from liquid.A constituents, especially. when the liquid constituents;y are of emergecousnature'.
  • the viscosity of a liquid varies, appreciably depending upon temperature, the:variation.l
  • the present invention is particularly adapted,y for the handling of liquids which have viscosities in excess. of about 200 seconds ⁇ Saybolt Universal at100F. Viscous liquids having Furol, viscosities in ⁇ excessof about 30 seconds at 275 F; are also, eiliciently handled by the present process.
  • One direct application of the present invention is in the manufacture of high qualityy asphaltsy in a process wherein a liquified normally gaseous hydrocarbon is employed in the manufacture of the asphalts and wherein the liquified hydro.- carbon is removed from they product stream. by a.
  • the size of the resilient mass employed, as pointed out heretofore, may vary appreciably. However, in general it is preferred that the dimensions of the sides of the face of the mass upon which the stream is impinged be from about 1% to three times the diameter of the owing stream. The thickness or depth of the mass likewise should be from about 1/2 to 11A times the diameter of the flowing stream impinged thereon.
  • Process for the separation of entrapped gaseous constituents from a viscous liquid flowing in a conduit said viscous liquid being characterized by having a viscosity from about 30- 1200 seconds Furol at 300 F. which comprises heating said viscous liquid to a temperature above the vaporization temperature of said entrapped gaseous constituents, passing said heated viscous liquid from said conduit through a vapor space at a high velocity into a separation Zone and impinging said viscous liquid onto and into a resilient mass of a lamentous material maintained in said separation zone, said mass being characterized by having a thickness in the range from about 3 inches to l2 inches and being further characterized by having at least 50% free space, whereby separation of said gaseous constituents and the viscous liquid is secured, removing the gaseous constituents from the top of said separation zone and said viscous liquid from the bottom of said separation zone.
  • an apparatus for disengaging a gaseous fluid from a liquid in which the said liquid and gaseous fluid is introduced to an intermediate level of a vertically elongated disengagement vessel through a conduit inlet at a sufiiciently high ow rate to enter the said Vessel as a solid iiuid stream the improvement which comprises a mass of fine filamentous solids positioned within said vessel directly in line with fluid ow from the said 8 inlet, said lamentous solids being characterized by a free space of more than about and having a filament diameter in the range of about 0.005 inch to 0.02 inch, said mass of filamentous solids being spaced from the said inlet at a distance of about 1 to 3 times the diameter of the said inlet, whereby said fluid stream impinges directly on said lamentous mass causing said gaseous fluid and liquid to disengage to permit removal of gas from the upper portion of said vessel, and liquid from the bottom portion of said vessel.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US77172A 1949-02-18 1949-02-18 Separation of vapors and viscous liquids Expired - Lifetime US2669538A (en)

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BE493780D BE493780A (en(2012)) 1949-02-18
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Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2958220A (en) * 1955-05-11 1960-11-01 Ruska Instr Corp Test separation of gas and liquid
US3972807A (en) * 1975-06-25 1976-08-03 Universal Oil Products Company Hydrocarbon deasphalting via solvent extraction
US4324651A (en) * 1980-12-09 1982-04-13 Mobil Oil Corporation Deasphalting process
US4536283A (en) * 1984-08-20 1985-08-20 Exxon Research And Engineering Co. Integrated process for deasphalting heavy oils using a gaseous antisolvent
US4565623A (en) * 1984-08-20 1986-01-21 Exxon Research And Engineering Co. Method for deasphalting heavy oils using a miscible solvent at a low treat ratio and a carbon dioxide antisolvent
US4572781A (en) * 1984-02-29 1986-02-25 Intevep S.A. Solvent deasphalting in solid phase
WO1998011971A1 (en) * 1996-09-19 1998-03-26 Ormat Process Technologies, Inc. Process and apparatus for solvent-deasphalting residual oil containing asphaltenes

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1240385A (en) * 1914-05-09 1917-09-18 Ernest J Sweetland Filter.
US1255018A (en) * 1916-03-30 1918-01-29 Philip Jones Process and apparatus for the separation of oils and gases.
US1379056A (en) * 1917-01-29 1921-05-24 Gas Res Co Purification of gas
FR529990A (fr) * 1913-11-11 1921-12-10 Procédé et dispositif pour l'élimination de l'air et des gaz des liquides, notamment de l'eau d'alimentation de chaudières
US1463990A (en) * 1923-08-07 louis
US2018871A (en) * 1933-03-30 1935-10-29 Ig Farbenindustrie Ag Production of high quality lubricating oils
US2110845A (en) * 1932-05-23 1938-03-08 Standard Oil Dev Co Treatment of heavy hydrocarbon oils with light hydrocarbons
US2420115A (en) * 1944-06-10 1947-05-06 Jay P Walker Methods of and apparatus for treating oil well streams

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1463990A (en) * 1923-08-07 louis
FR529990A (fr) * 1913-11-11 1921-12-10 Procédé et dispositif pour l'élimination de l'air et des gaz des liquides, notamment de l'eau d'alimentation de chaudières
US1240385A (en) * 1914-05-09 1917-09-18 Ernest J Sweetland Filter.
US1255018A (en) * 1916-03-30 1918-01-29 Philip Jones Process and apparatus for the separation of oils and gases.
US1379056A (en) * 1917-01-29 1921-05-24 Gas Res Co Purification of gas
US2110845A (en) * 1932-05-23 1938-03-08 Standard Oil Dev Co Treatment of heavy hydrocarbon oils with light hydrocarbons
US2018871A (en) * 1933-03-30 1935-10-29 Ig Farbenindustrie Ag Production of high quality lubricating oils
US2420115A (en) * 1944-06-10 1947-05-06 Jay P Walker Methods of and apparatus for treating oil well streams

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2958220A (en) * 1955-05-11 1960-11-01 Ruska Instr Corp Test separation of gas and liquid
US3972807A (en) * 1975-06-25 1976-08-03 Universal Oil Products Company Hydrocarbon deasphalting via solvent extraction
US4324651A (en) * 1980-12-09 1982-04-13 Mobil Oil Corporation Deasphalting process
US4572781A (en) * 1984-02-29 1986-02-25 Intevep S.A. Solvent deasphalting in solid phase
US4536283A (en) * 1984-08-20 1985-08-20 Exxon Research And Engineering Co. Integrated process for deasphalting heavy oils using a gaseous antisolvent
US4565623A (en) * 1984-08-20 1986-01-21 Exxon Research And Engineering Co. Method for deasphalting heavy oils using a miscible solvent at a low treat ratio and a carbon dioxide antisolvent
WO1998011971A1 (en) * 1996-09-19 1998-03-26 Ormat Process Technologies, Inc. Process and apparatus for solvent-deasphalting residual oil containing asphaltenes
US5914010A (en) * 1996-09-19 1999-06-22 Ormat Industries Ltd. Apparatus for solvent-deasphalting residual oil containing asphaltenes

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